Design og modellering af metanolanlæg til VEnzin-visionen Bilag

27.07.2013 Views
0 1 1 1 P 2 M type NOD* 1 1 type NOD* 1 1 1 Energy flow 2 Cost flow type NOD* 1 2 1 Exergy efficiency 2 Exergy destruction Water Steam 3T 2 1 3Exergy destruction cost flow - based on specific cost of input 4.6 0.228 2.0 3.73 4H 3 0 4Exergy destruction cost flow - based on specific cost of output 1 1.0 bar Electrolyser 423 10.0 bar 11.24 412 2 5EX 5 Component cost flow 2 4.6 kg/s 76.6 MW 201 2 2.0 kg/s 10.1 10.0 bar Biogas 6 EX_CH * Number of decimals Electrolyser 0.146 15 C SAND 76.58 0.07 850 C 226.6 10.1 kg/s 7 EX_PH SAND 301 Electrolyser NG_reformer 891 C 8X 9 EX*M 10 EX_CH*M Comp-O2-1 DH water 0.281 803 4 19.5 1.0 bar Electrolyser 25.31 3.3 0.79 0 802 2 19.5 1.0 bar DH water 0.93 Steam reformer 12.66 NG_reformer O2 11 EX_PH*M 0.0 MW 1 0.679 19.5 kg/s 4.1 0.534 0.5 59.87 0.16 19.5 kg/s 3.9 2.985 12 C 13 C/EX SAND 1E-08 90 C Electro-cool 3 4 1.0 bar 4.1 kg/s 2 4 1.0 bar 0.5 kg/s 50 C Electro-cool Comp-O2-2 1.3 MW 3 Reformat 16.1 217 403 2 10.0 bar 3.9 kg/s 0.0 0 Ash 0.0 2E-04 83 1.0 bar 4 0.0 kg/s 14 C/M O2 5E-05 7 4 5E-05 0.90 0.0 1.0 bar 1E-04 0.0 kg/s 90 C Comp-O2-1 5E-05 5 2 0.0 1.0 bar 1E-04 0.0 kg/s 90 C Comp-O2-1 DH water Gas 0.221 90 C Electrolyser 0.1 0.015 6 1.0 bar 4 0.1 kg/s 24.8 90 C Electrolyser H2 O2 0.215 401 2 3.9 1.0 bar 0.519 3.9 kg/s 90 C SAND 1.346 0.692 402 4 0.94 0.692 3.9 10.0 bar 1.782 3.9 kg/s 431 C 431 10.0 bar 4 16.1 kg/s 12.66 950 C NG_reformer 0.69 850 C NG_reformer 1.7 23.44 441 10.0 bar 2 1.7 kg/s 1.367 950 C Heatex-O2 Gasifier 304 0.0 MW SAND 0 800 C Gasifier 0.0 5E-05 0.0 33 2 1.0 bar Steam 32 0.0 0.009 1.0 bar 801 2 0.0 4E-05 1.0 bar 0.0 kg/s 15 4 0.0 1E-05 1.0 bar 0.0 kg/s Heatsink-H2 0.006 90 C Split-O2-2 O2 0.90 Comp-H2 Comp-O2-2 Comp-O2-2 432 2 9.9 134 10.0 bar 9.9 kg/s 1.8 0.69 0.97 Heatex-O2 SAND 11 0.001 0.0 kg/s Heatex-GG-st 4 0.0 kg/s 0 50 C 0 60 C 0.0 MW 322 24.8 0.0 MW 9 Comp-CO2 7.818 950 C 730 C SAND 7 0.00 730 C Heatex-GG-DH Cleaner SAND 0.0 SAND 9E-05 0.0 MW 7 Heatex-NG 0.89 0 Gasifier 0.0 0.115 0 0.0 0.104 Gasifier 10 GG2 0.00 0.78 1.0 bar 0.0 0.0 kg/s 800 C 0 0.0 0.104 11 2 1.0 bar 0.0 kg/s 752 C Heatex-GG-st 0.00 0.99 0 0.0 0.0 0.099 12 2 0.00 0.74 1.0 bar 0.0 0.0 kg/s 130 C Heatex-GG-DH 0 0.0 0.099 13 2 1.0 bar 0.0 kg/s 60 C 1.00 Gas cleaner 0.0 0.0 0.099 14 1.0 bar 0.00 Heatsink 24.80 24.8 511 2 0.5 1.0 bar 59.87 0.5 kg/s 90 C Heatsink-H2 13.79 503 4 15.4 21.2 bar SAND 0.003 0.002 502 4 0.002 0.001 501 2 0.93 0.0 21.2 bar 0.0 1.0 bar CO2 11.22 411 2 Biogas 10.1 10.0 bar 215.8 10.1 kg/s 25 C Heatex-NG 451 Heatex-NG SAND 4.4 59.5 10.0 bar 18.6 13 11.24 0.99 0 434 Water 2 0.5 10.0 bar 82 1.0 bar Heatex-GG-O2 Heatex-GG-st Heatex-GG-DH SAND 9 Cleaner 4 0.0 kg/s 202.6 15.4 kg/s 0.007 0.0 kg/s 0.005 0.0 kg/s 2 4.4 kg/s 0.047 0.5 kg/s 2 0.0 kg/s 0.00 9 2 Heatex-GG-O2 0.0 0.004 0 21 4 0.0 60 C 254 C 286 C 15 C 3.471 950 C 107 C 0.00 120 C 0.0 1.0 bar SAND 5 31 1.0 bar 0.0 1.0 bar Cleaner 24.80 512 2 26.06 524 4 15.9 265 Mixer-CO2-NG Comp-CO2 Comp-CO2 Heatex-H2O Pres-sep-3 Gasifier H2O [mass-%] = 0.05 Dry-wood 5E-04 0.0 kg/s 790 C Gasifier 2 0.0 kg/s 3E-04 120 C Heatex-GG-st -0 0.0 kg/s 60 C 521 Heatex-GG-DH 2 0.5 59.97 1.0 bar 0.5 kg/s 0.5 59.87 1.0 bar 0.5 kg/s 90 C 0.5 62.82 21.2 bar 0.5 kg/s 403 C 531 2 39.86 21.2 bar 15.9 kg/s 283 C 0.065 422 2 Water 2.0 10.0 bar 0.115 2.0 kg/s 8.3 Heatex-H2O 0.07 0.75 SAND 15 0 453 Water 4 Steam 811 0.0 2E-04 1.0 bar 24.81 90 C Comp-GG-H2-1 Comp-GG-H2-1 1.5 MW 11 Mixer-GG-H2 Comp-GG-H2-2 36.5 24.44 Syngas-cool1 45 C Heatex-H2O 0.2 0.02 10.0 bar 0.2 kg/s 4 0.0 kg/s 0.93 SAND 1.463 571 1.0 bar Syngas-cool1 Comp-NG_ref 107 C 0.00 90 C 25.33 7.2 4.415 6 36.5 kg/s SAND 21 3.2 MW 5 4.2 Heatex-H2O 9.5 123.1 1.7 0.0 0.008 Heatex-GG-DH 0.5 61.33 563 1.0 bar 1.59 200 C 5.8 SAND 3.205 4.2 54.64 9.5 123.1 1.7 22.19 0.00 0.0 Steam_dryer Biomass (dry) SAND 1 35 4 0.50 0.0 0.00 34 2 1.0 bar Steam dryer 0.00 0.0 1.0 bar 34 1.0 bar 4 0.0 kg/s 2E-04 730 C Split-steam2 522 4.0 bar 2 0.5 kg/s 25.33 283 C Cooler-GG-H2 2 7.2 kg/s 0.31 120 C Cooler-GG-H2 1.1 0.31 0.84 25.33 523 2 0.5 4.0 bar 0.94 26.06 Syngas-cool1 561 2 1.589 36.5 22.51 1.0 bar 36.5 kg/s 120 C 1.59 0.84 0 541 4 0.0 21.2 bar -0 0.0 kg/s 130 C Water Reformat 13.79 462 2 13.79 15.4 21.2 bar 202.6 15.4 kg/s 12.66 461 2 0.93 15.4 10.0 bar 199.6 15.4 kg/s 452 10.0 bar 2 4.2 kg/s 3.471 107 C Mixer-NG_ref 433 10.0 bar 2 9.5 kg/s 7.818 107 C Mixer-NG_ref 442 10.0 bar 2 1.7 kg/s 1.367 483 C Mixer-NG_ref 0.03 0.0 kg/s 0.033 0.0 kg/s Cooler-GG-H2 7.2 4.793 60.88 0.5 kg/s Syngas-cool1 15.9 262.7 Syngas-cool1 254 C 151 C 120 C 0.0 0.115 271 C SAND 19 571 1.0 bar 130 C Comp-GG-H2-2 532 21.2 bar Mixer-CO2-NG Comp-NG_ref Steam_dryer 81 1.0 bar Steam_dryer 4 7.2 kg/s Comp-GG-H2-2 2 15.9 kg/s 2 0.003 0.0 kg/s 15 C Steam 0.31 200 C Cooler-GG-H2 2.1 MW SAND 13 2.072 39.86 130 C Comp-syngas1 Comp-syngas1 Component information Technical lifetime = O&M = 15 years 0.02 of the componentprice per year Operating hours = 8000 Exergy Steam DH-condenser Steam_dryer Biomass (wet) 0.0 0.002 41 1.0 bar 2 0.0 kg/s Steam 0.93 41.96 15.9 268.2 533 63.3 bar 4 15.9 kg/s Syngas 41.96 283 C 5.9 MW SAND 15 5.921 Electrolyser Comp-H2 Comp-O2-1 Node before component 1 2 5 Component type Electrolyser Compressor Compressor DNA name ELECTROLYSER COMPRE_1 COMPRE_1 Specific price 1.52 mio. kr/MWe 4.50 mio. kr/MW 4.50 mio. kr/MW Price [mio. kr] 116 0 0 Total price [mio. kr] 151 0 0 C [kr/s] 0.35 0.00 0.00 Input: Biogas Biomass Power* Total power * for electrolyser 216 MW 0 MW 77 MW 96 MW Output: Methanol DH Oxygen Syngas 231 MW 11 MW 0 MW 14 MW SAND 79 2E-04 120 C 94.1 62.97 set_temp-2 Gasifier 9 Gasifier GASIFI_3 3.80 mio. kr/MW-biomass 0 0 0.00 DH-condenser 0.91 0.0 0.28 811 12 DH condenser0.28 19.5 1.0 bar 581 2 4.10 1.0 bar 94.1 kg/s 200 C Steam 2.16 571 8 Heatex-GG-O2 Heatex-GG-st Heatex-GG-DH 10 11 12 Heat exchanger Heat exchanger Heat exchanger HEATEX_2 HEATEX_2 GASCOOL2 0.40 mio. kr/MW-transferred 0.40 mio. kr/MW-transferred 0.40 mio. kr/MW-transferred 0 0 0 0 0 0 0.00 0.00 0.00 Methanol-efficiency 1: Methanol-efficiency 2: Total efficiency: 79% (with power for electrolyser) 74% (with total power) 82% 0.0 3E-04 0.681 19.5 kg/s DH-cooler DH-cooler 49.4 1.0 bar Cleaner 13 Gas cleaner GASCLE_2 0.00 mio. kr/(kg/s)-gas 0 0 0.00 42 1.0 bar 90 C SAND 25 33.07 49.4 kg/s Steam_dryer 34 Steam dryer DRYER_04 4.10 mio. kr/(kg/s)-evaporated 0 0 0.00 4 0.0 kg/s 0 95 C DH-condenser DH-condenser 407.0 14.22 811 1.0 bar 0.018 811 6 89.5 1.0 bar 3.126 89.5 kg/s 0.48 15.0 0 804 2 DH cooler DH water 0.02 89.5 1.0 bar 0.733 89.5 kg/s 1.0 0.689 2.15 562 2 49.4 1.0 bar 200 C Syngas-cool2 7.9 2.16 0.90 Syngas-cool2 SAND 23 DH-condenser Comp-O2-2 Heatex-O2 41 401 402 Heat exchanger Compressor Heat exchanger HEATEX_1 COMPRE_1 HEATEX_4 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 0.40 mio. kr/MW-transferred 0 6 1 0 8 1 0.00 0.02 0.00 Energy Water 2 407.0 kg/s 0.36 90 C DH DH water 90 C DH-cooler 35 6 94.1 57.98 1.0 bar 94.1 kg/s 50 C DH-cooler 571 1.0 bar 10 1.0 kg/s 0.04 225 C Cond-steam-1 30.46 49.4 kg/s 120 C Syngas-cool2 534 2 14.8 265.1 63.3 bar 14.8 kg/s 0 551 4 1.1 63.3 bar 0.165 1.1 kg/s 141 C NG_reformer Heatex-NG Water Heatex-H2O Comp-NG_ref Comp-CO2 403 411 422 461 501 NG reformer Heat exchanger Heat exchanger Compressor Compressor STEAM_REFORMER GASCOOL2 GASCOOL2 COMPRE_1 COMPRE_1 1.05 mio. kr/MW-NG 0.40 mio. kr/MW-transferred 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 4.50 mio. kr/MW 213 7 3 14 0 277 10 4 19 0 0.64 0.02 0.01 0.04 0.00 Input: Biogas Biomass Power* Total power 204 MW 0 MW 77 MW 96 MW Output: Methanol DH Oxygen Syngas 205 MW 68 MW 0 MW 12 MW Energy content in DH water = 68 MW 4.10 120 C DH-cooler Steam 41.96 141 C Comp-syngas2 Syngas-cool2 Heatsink-H2 Comp-GG-H2-1 511 521 Heat exchanger Compressor HEATSNK0 COMPRE_1 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 0 7 0 9 0.00 0.02 * for electrolyser Urenhed: 0.035 % Methanol loss in distillation [%] = 1.0 Methanol molar-% = 99.96 Water / 671 1.0 0.616 1.0 bar 0.93 43.43 14.8 Comp-syngas2 4.2 MW 17 SAND 4.157 269 Cooler-GG-H2 Comp-GG-H2-2 Syngas-cool1 Comp-syngas1 522 523 531 532 Heat exchanger Compressor Heat exchanger Compressor GASCOOL2 COMPRE_1 GASCOOL2 COMPRE_1 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 0 9 2 27 1 12 3 35 0.00 0.03 0.01 0.08 Methanol-efficiency 1: Methanol-efficiency 2: Total efficiency: 73% (with power for electrolyser) 68% (with total power) 95% Methanol 2 1.0 kg/s 535 144.0 bar Syngas-cool2 533 Heat exchanger GASCOOL2 0.40 mio. kr/MW-transferred 3 4 0.01 0.04 120 C 2 14.8 kg/s Comp-syngas2 534 Compressor COMPRE_1 4.50 mio. kr/MW 19 24 0.06 Cond-steam-1 43.43 255 C Meoh-convert 601 Meoh converter MEOH_CONVERTER ##### mio. kr/(kmol/s-syngas) 361 469 1.08 Gas composition at specific nodes (mol-%) 43.01 10.3 231.1 set-M Preheater-sy 602 Heat exchanger GASCOOL4 0.40 mio. kr/MW-transferred 4 6 0.01 793 794 3.5 bar 10.3 kg/s 601 68.5 531.9 144.0 bar Condenser-1 Syngas Condenser 640 643 Heat exchanger Heat exchanger GASCOOL4 GASCOOL4 0.40 mio. kr/MW-transferred 0.40 mio. kr/MW-transferred 3 5 3 6 0.01 0.01 Node 10 3 15 431 534 601 602 640 643 605 15 23 33 35 41 43 39 37 M-factor 1.60 4 100 C 2 68.5 kg/s Comp-recirc 605 Compressor COMPRE_1 4.50 mio. kr/MW 1 1 0.00 Species Split-meoh1 155.3 37.2 834.4 Steam 0 682 4 91 235 C Meoh-convert feed_Water Cond-steam-1 625 671 Distillation column Heat exchanger DISTILLATION_STAGE* HEATEX_1 23.52 mio. kr/(kg/s-feed) 0.40 mio. kr/MW-transferred 282 0 366 0 0.85 0.00 1 3 H2 N2 45.98 0.25 0.00 46.10 60.37 41.82 24.69 26.26 27.85 30.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 791 3.5 bar 16.8 30.6 bar Cond-steam-2 685 Heat exchanger HEATSNK0 0.40 mio. kr/MW-transferred 12 16 0.04 4 CO 42.73 0.00 31.87 26.62 12.44 2.80 2.98 3.16 3.41 792 37.2 kg/s 17.17 16.8 kg/s DH-cooler 804 Heat exchanger HEATEX_1 0.40 mio. kr/MW-transferred 6 8 0.02 6 CO2 5.24 0.00 8.15 6.82 40.23 50.62 53.85 57.11 61.51 Heatsourc-DH 4 100 C Cond-steam-1 235 C Heatsourc-DH 806 Heat exchanger HEATSRC0 0.40 mio. kr/MW-transferred 15 20 0.05 7 H2O-G 5.21 0.00 13.43 5.81 2.28 3.78 2.10 0.88 0.03 SAND 390 Cond-meoh SAND 35 Convert-cool * The distillation column is composed of 9 H2S 0.00 ##### 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.046 811 10 38.0 226.9 1.0 bar 0.046 0.70 0 806 2 DH water 226.9 1.0 bar 0 683 2 0.1 30.6 bar 0.2 0.04 0.81 0 684 4 0.1 30.6 bar Water 0 681 2 16.8 30.6 bar 31.1 Meoh-convert Methanol 1.00 SAND converter 92 311 Total several DISTILLATION_STAGE's 1118 1426 3.36 11 36 40 CH4 AR CH3OH 0.48 0.12 0.00 0.00 0.00 0.00 0.45 0.00 0.00 0.37 0.00 0.00 2.90 3.71 3.95 0.00 0.00 0.00 0.33 14.40 10.85 4.19 0.00 6.80 4.51 0.00 0.54 7.927 226.9 kg/s 90 C 1.858 226.9 kg/s 50 C 0.115 0.1 kg/s 235 C 0.025 0.1 kg/s 220 C 3.691 16.8 kg/s 220 C 602 68.5 517 139.0 bar 607 53.7 264.5 144.0 bar Input prices GG H2S NG_ref-cool Syngas-loop1 Syngas-meoh- Syngas-loop2 Syngas-3 Syngas-meoh Syngas-loop3 112.3 Heatsourc-DH 155.3 26.9 603.3 783 37.2 843.1 Heatsourc-DH 3.5 bar Cond-steam-1 Cond-steam-1 Convert-cool 2 92 68.5 kg/s 235 C 2 47 53.7 kg/s 225 C Input Electric power Price 324 kr/GJ Output cost Comparable fuel prices 781 3.5 bar 784 37.2 kg/s 16.6 17.05 Preheater-sy Mixer-syn_re Mechanical power 341 kr/GJ Output Cost flow Cost (exergy) Cost (energy) Cost (mass) Cost (volume) Fuel Price (exergy) Price (volume) 782 26.9 kg/s 4 100 C 685 30.6 bar 11.1 Preheater-sy Biogas 55 kr/GJ Methanol 43.0 kr/s 186 kr/GJ 210 kr/GJ 4.18 kr/kg 3.3 kr/l Methanol (commercial) 142 kr/GJ 2.5 kr/l 2 100 C Dis_stage_17 2 16.6 kg/s 47 606 2 47 0.87 SAND 29 Biomass 32 kr/GJ Oxygen 0.0 kr/s 414 kr/GJ - kr/GJ 0.05 kr/kg - kr/l Petrol 187 kr/GJ 6.6 kr/l Dis_stage_17 0 235 C Comp-recirc 47 53.7 144.0 bar 64.6 442.4 DH water 0 kr/ton Syngas 2.5 kr/s 181 kr/GJ - kr/GJ 0.88 kr/kg - kr/l Crude oil 58 kr/GJ 2.2 kr/l Cond-steam-2 0.2 MW 19 0.90 261.2 53.7 kg/s 640 139.0 bar 70 12.66 3.9 70.75 Water 32 kr/ton DH water 0.4 kr/s 25 kr/GJ 5 kr/GJ 0.00 kr/kg - kr/l Ethanol 100 kr/GJ 2.4 kr/l 0 681 4 SAND 0.203 63 C 2 64.6 kg/s 621 139.0 bar CO2 114 kr/ton Water 0 kr/s - kr/GJ - kr/GJ - kr/kg - kr/l Distillation column 161 0.71 Feed 16.6 3.667 30.6 bar 16.6 kg/s 220 C Preheater-sy 79.14 168 C Condenser-1 6.3 631 3.9 kg/s 4 168 C Preheater-sy Nomenclature: Cond-steam-2 0.93 1.03 If methanol and DH share the plant costs Condenser-1 77.8 12.57 621 631 4 (methanol and DH are the only products from the plant) - 5 705 706 18 3.5 bar 2 0.93 705 706 3 3.5 bar 6 SAND 31 61.0 370.6 643 139.0 bar 2 61.0 kg/s 4 139.0 bar 70 3.6 kg/s 144 C and the DH cost is fixed corresponding to the DH price: Output Cost flow Cost Methanol 35.6 kr/s 154 kr/Gjex Electrical power Node nr Pressure Transferred heat [MW] 38 17.8 kg/s 6 3.0 kg/s Condenser 66.57 144 C Preheater-sy DH water 10.3 kr/s 150 kr/Gjen Mass flow 134 C 134 C SAND 33 Condenser Temperature Dis_stage_1 0.01 811 8 71.2 1.0 bar Reboil-meoh2 11.9 0.01 0.75 0 805 2 DH water 71.2 1.0 bar Mechanical power 10 5.455 19.5 29.62 2.487 71.2 kg/s 0.583 71.2 kg/s 0.919 3.0 4.559 707 3.5 bar Cond-steam-2 90 C 47.2 605 2 50 C 699 3.5 bar 0.25 708 19.5 kg/s SAND 393 Condenser 53.7 139.0 bar 2.8 13.74 Condenser 700 3.0 kg/s 4 134 C 261 53.7 kg/s 611 139.0 bar 88.0 16.89 4.5 93.4 2 134 C Water / Methanol Methanol molar-% = 3.59 0 693 694 2 3.5 bar 3 1.7 kg/s Dis_stage_1 4 4.537 695 696 15 3.5 bar 23 14.8 kg/s 2 30.9 4.574 0.67 4.574 705 706 15 3.5 bar 32 14.8 kg/s 4 42.12 625 635 12 3.5 bar 2 Methanol molar-% = 78.8 60 C Comp-recirc Methanol/ 4 2.8 kg/s 2.484 60 C Syngas Split-syngas 621 139.0 bar 631 4.5 kg/s 4 60 C Preheater-sy Reboil-meoh2 Heat Exergy efficiency [-] 64 C set-x-2 134 C Reboil-meoh1 134 C Reboil-meoh1 234 12.0 kg/s 102 C meas_flow Methanol mass flow = 10.4 kg/s water

0 1 1 1 P 2 M type NOD* 1 1 type NOD* 1 1 1 Energy flow 2 Cost flow type NOD* 1 2 1 Exergy efficiency 2 Exergy destruction Water Steam 3T 2 1 3Exergy destruction cost flow - based on specific cost of input 18.6 -0 0.0 0.006 4H 3 0 4Exergy destruction cost flow - based on specific cost of output 1 1.0 bar Electrolyser 423 10.0 bar 0.02 412 2 5EX 5 Component cost flow 2 18.6 kg/s 311.6 MW 201 2 0.0 kg/s 0.0 10.0 bar NG 6 EX_CH * Number of decimals Electrolyser 0.594 15 C SAND 311.6 0.00 850 C 0.176 0.0 kg/s 7 EX_PH SAND 301 Electrolyser NG_reformer 667 C 8X 9 EX*M 10 EX_CH*M Comp-O2-1 DH water 1.144 803 4 79.1 1.0 bar Electrolyser 103 13.2 0.80 0 802 2 79.1 1.0 bar DH water 0.93 Steam reformer 0.02 NG_reformer O2 11 EX_PH*M 0.0 MW 1 2.762 79.1 kg/s 16.5 2.174 2.1 243.6 0.648 79.1 kg/s 0.0 0.002 12 C 13 C/EX SAND 1E-08 90 C Electro-cool 3 4 1.0 bar 16.5 kg/s 2 4 1.0 bar 2.1 kg/s 50 C Electro-cool Comp-O2-2 0.0 MW 3 Reformat 0.0 0.171 403 2 10.0 bar 0.0 kg/s 0.0 0 Ash 0.0 2E-04 83 1.0 bar 4 0.0 kg/s 14 C/M O2 5E-05 7 4 5E-05 0.90 0.0 1.0 bar 1E-04 0.0 kg/s 90 C Comp-O2-1 5E-05 5 2 0.0 1.0 bar 1E-04 0.0 kg/s 90 C Comp-O2-1 DH water Gas 0.901 90 C Electrolyser 16.5 2.173 6 1.0 bar 4 16.5 kg/s 100.9 90 C Electrolyser H2 O2 2E-04 401 2 0.0 1.0 bar 4E-04 0.0 kg/s 90 C SAND 0.001 6E-04 402 4 0.94 6E-04 0.0 10.0 bar 0.001 0.0 kg/s 431 C 431 10.0 bar 4 0.0 kg/s 0.02 950 C NG_reformer 0.00 850 C NG_reformer 0.0 0.019 441 10.0 bar 2 0.0 kg/s 0.002 950 C Heatex-O2 Gasifier 304 0.0 MW SAND 0 800 C Gasifier 0.0 3E-05 0.0 33 2 1.0 bar Steam 32 0.0 0.009 1.0 bar 801 2 0.0 4E-05 1.0 bar 0.0 kg/s 15 4 0.0 1E-05 1.0 bar 0.0 kg/s Heatsink-H2 0.9 90 C Split-O2-2 O2 0.90 Comp-H2 Comp-O2-2 Comp-O2-2 432 2 0.0 0.05 10.0 bar 0.0 kg/s 0.0 0.00 0.97 Heatex-O2 SAND 11 0.001 0.0 kg/s Heatex-GG-st 4 0.0 kg/s 0 50 C 0 60 C 0.0 MW 322 100.9 0.0 MW 9 Comp-CO2 0.005 950 C 730 C SAND 7 0.00 730 C Heatex-GG-DH Cleaner SAND 0.0 SAND 4E-04 4.4 MW 7 Heatex-NG 0.89 0 Gasifier 0.0 0.115 0 0.0 0.104 Gasifier 10 GG2 0.00 0.78 1.0 bar 0.0 0.0 kg/s 800 C 0 0.0 0.104 11 2 1.0 bar 0.0 kg/s 752 C Heatex-GG-st 0.00 0.99 0 0.0 0.0 0.099 12 2 0.00 0.74 1.0 bar 0.0 0.0 kg/s 130 C Heatex-GG-DH 0 0.0 0.099 13 2 1.0 bar 0.0 kg/s 60 C 1.00 Gas cleaner 0.0 0.0 0.099 14 1.0 bar 0.00 Heatsink ##### 100.9 511 2 2.1 1.0 bar 243.6 2.1 kg/s 90 C Heatsink-H2 3.806 503 4 19.6 14.6 bar SAND 4.373 3.789 502 4 3.789 2.238 501 2 0.92 19.6 14.6 bar 19.6 1.0 bar CO2 0.015 411 2 NG0.0 10.0 bar 0.173 0.0 kg/s 25 C Heatex-NG 451 Heatex-NG SAND 0.0 0.102 10.0 bar 0.0 13 0.02 0.89 0 434 Water 2 0.0 10.0 bar 82 1.0 bar Heatex-GG-O2 Heatex-GG-st Heatex-GG-DH SAND 9 Cleaner 4 0.0 kg/s 13.05 19.6 kg/s 12.91 19.6 kg/s 8.864 19.6 kg/s 2 0.0 kg/s 1E-05 0.0 kg/s 2 0.0 kg/s 0.00 9 2 Heatex-GG-O2 0.0 0.004 0 21 4 0.0 60 C 248 C 248 C 15 C 0.01 950 C 107 C 0.00 120 C 0.0 1.0 bar SAND 5 31 1.0 bar 0.0 1.0 bar Cleaner ##### 512 2 105.2 524 4 21.7 263.9 Mixer-CO2-NG Comp-CO2 Comp-CO2 Heatex-H2O Pres-sep-3 Gasifier H2O [mass-%] = 0.05 Dry-wood 5E-04 0.0 kg/s 790 C Gasifier 2 0.0 kg/s 2E-04 120 C Heatex-GG-st 1E-22 0.0 kg/s 60 C 521 Heatex-GG-DH 2 2.1 243.7 1.0 bar 2.1 kg/s 2.1 243.6 1.0 bar 2.1 kg/s 90 C 2.1 253.1 14.6 bar 2.1 kg/s 322 C 531 2 109 14.6 bar 21.7 kg/s 292 C 1E-04 422 2 Water 0.0 10.0 bar 1E-05 0.0 kg/s 0.0 Heatex-H2O 0.00 0.74 SAND 15 0 453 Water 4 Steam 811 0.0 2E-04 1.0 bar ##### 90 C Comp-GG-H2-1 Comp-GG-H2-1 6.2 MW 11 Mixer-GG-H2 Comp-GG-H2-2 50.9 31.51 Syngas-cool1 33 C Heatex-H2O 0.0 2E-05 10.0 bar 0.0 kg/s 4 0.0 kg/s 0.93 SAND 6.215 571 1.0 bar Syngas-cool1 Comp-NG_ref 109 C 0.00 90 C 103.1 30.8 17.44 6 50.9 kg/s SAND 21 0.0 MW 5 0.0 Heatex-H2O 0.0 0.046 0.0 0.0 0.007 Heatex-GG-DH 2.1 249.5 563 1.0 bar 1.32 200 C 8.1 SAND 0.001 0.0 0.094 0.0 0.046 0.0 0.018 0.00 0.0 Steam_dryer Biomass (dry) SAND 1 35 4 0.46 0.0 0.00 34 2 1.0 bar Steam dryer 0.00 0.0 1.0 bar 34 1.0 bar 4 0.0 kg/s 1E-04 730 C Split-steam2 522 4.2 bar 2 2.1 kg/s 103.1 292 C Cooler-GG-H2 2 30.8 kg/s 0.80 120 C Cooler-GG-H2 4.9 0.81 0.83 ##### 523 2 2.1 4.2 bar 0.93 105.2 Syngas-cool1 561 2 1.322 50.9 28.82 1.0 bar 50.9 kg/s 120 C 1.33 0.83 0 541 4 0.0 14.6 bar 7E-21 0.0 kg/s 130 C Water Reformat 0.017 462 2 0.017 0.0 14.6 bar 0.159 0.0 kg/s 0.017 461 2 0.92 0.0 10.0 bar 0.158 0.0 kg/s 452 10.0 bar 2 0.0 kg/s 0.01 109 C Mixer-NG_ref 433 10.0 bar 2 0.0 kg/s 0.005 107 C Mixer-NG_ref 442 10.0 bar 2 0.0 kg/s 0.002 483 C Mixer-NG_ref 0.028 0.0 kg/s 0.03 0.0 kg/s Cooler-GG-H2 30.8 19.06 247.5 2.1 kg/s Syngas-cool1 21.7 260.7 Syngas-cool1 206 C 154 C 120 C 0.0 0.115 271 C SAND 19 571 1.0 bar 130 C Comp-GG-H2-2 532 14.6 bar Mixer-CO2-NG Comp-NG_ref Steam_dryer 81 1.0 bar Steam_dryer 4 30.8 kg/s Comp-GG-H2-2 2 21.7 kg/s 2 0.003 0.0 kg/s 15 C Steam 0.81 200 C Cooler-GG-H2 5.9 MW SAND 13 5.922 109 130 C Comp-syngas1 Comp-syngas1 Component information Technical lifetime = O&M = 15 years 0.02 of the componentprice per year Operating hours = 8000 Exergy Steam DH-condenser Steam_dryer Biomass (wet) 0.0 0.002 41 1.0 bar 2 0.0 kg/s Steam 0.93 112 21.7 268.4 533 51.1 bar 4 21.7 kg/s Syngas112 292 C 8.2 MW SAND 15 8.248 Electrolyser Comp-H2 Comp-O2-1 Node before component 1 2 5 Component type Electrolyser Compressor Compressor DNA name ELECTROLYSER COMPRE_1 COMPRE_1 Specific price 1.52 mio. kr/MWe 4.50 mio. kr/MW 4.50 mio. kr/MW Price [mio. kr] 474 0 0 Total price [mio. kr] 616 0 0 C [kr/s] 1.43 0.00 0.00 Input: NG Biomass Power* Total power * for electrolyser 0 MW 0 MW 312 MW 345 MW Output: Methanol DH Oxygen Syngas 231 MW 13 MW 2 MW 18 MW SAND 79 1E-04 120 C 133.5 82.69 set_temp-2 Gasifier 9 Gasifier GASIFI_3 3.80 mio. kr/MW-biomass 0 0 0.00 DH-condenser 0.91 0.0 1.14 811 12 DH condenser1.14 79.1 1.0 bar 581 1.0 bar 2 133.5 kg/s 3.48 200 C Steam 1.33 571 8 Heatex-GG-O2 Heatex-GG-st Heatex-GG-DH 10 11 12 Heat exchanger Heat exchanger Heat exchanger HEATEX_2 HEATEX_2 GASCOOL2 0.40 mio. kr/MW-transferred 0.40 mio. kr/MW-transferred 0.40 mio. kr/MW-transferred 0 0 0 0 0 0 0.00 0.00 0.00 Methanol-efficiency 1: Methanol-efficiency 2: Total efficiency: 74% (with power for electrolyser) 67% (with total power) 77% 0.0 1E-04 2.764 79.1 kg/s DH-cooler DH-cooler 50.9 1.0 bar Cleaner 13 Gas cleaner GASCLE_2 0.00 mio. kr/(kg/s)-gas 0 0 0.00 42 1.0 bar 90 C SAND 25 31.51 50.9 kg/s Steam_dryer 34 Steam dryer DRYER_04 4.10 mio. kr/(kg/s)-evaporated 0 0 0.00 4 0.0 kg/s 0 95 C DH-condenser DH-condenser 500.0 17.47 811 1.0 bar 0.026 811 6 126.9 1.0 bar 4.432 126.9 kg/s 0.48 21.3 0 804 2 DH cooler DH water 0.03 126.9 1.0 bar 1.039 126.9 kg/s 1.0 0.639 1.322 562 2 50.9 1.0 bar 200 C Syngas-cool2 8.1 1.33 0.83 Syngas-cool2 SAND 23 DH-condenser Comp-O2-2 Heatex-O2 41 401 402 Heat exchanger Compressor Heat exchanger HEATEX_1 COMPRE_1 HEATEX_4 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 0.40 mio. kr/MW-transferred 0 0 0 0 0 0 0.00 0.00 0.00 Energy Water 2 500.0 kg/s 1.23 90 C DH DH water 90 C DH-cooler 133.5 75.62 35 1.0 bar 6 133.5 kg/s 50 C DH-cooler 571 1.0 bar 10 1.0 kg/s 0.03 225 C Cond-steam-1 28.82 50.9 kg/s 120 C Syngas-cool2 534 2 21.7 265.1 51.1 bar 21.7 kg/s 0 551 4 0.0 51.1 bar -0 0.0 kg/s 130 C NG_reformer Heatex-NG Water Heatex-H2O Comp-NG_ref Comp-CO2 403 411 422 461 501 NG reformer Heat exchanger Heat exchanger Compressor Compressor STEAM_REFORMER GASCOOL2 GASCOOL2 COMPRE_1 COMPRE_1 1.05 mio. kr/MW-NG 0.40 mio. kr/MW-transferred 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 4.50 mio. kr/MW 0 0 0 0 20 0 0 0 0 26 0.00 0.00 0.00 0.00 0.06 Input: NG Biomass Power* Total power 0MW 0 MW 312 MW 345 MW Output: Methanol DH Oxygen Syngas 205 MW 84 MW 0 MW 14 MW Energy content in DH water = 84 MW 3.48 120 C DH-cooler Steam 112 130 C Comp-syngas2 Syngas-cool2 Heatsink-H2 Comp-GG-H2-1 511 521 Heat exchanger Compressor HEATSNK0 COMPRE_1 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 0 28 0 36 0.00 0.08 * for electrolyser Urenhed: 0.493 % Methanol loss in distillation [%] = 1.0 Methanol molar-% = 99.51 Water / 671 1.0 0.566 1.0 bar 0.93 Comp-syngas2 114.3 6.6 MW 17 SAND 6.637 21.7 271.3 Cooler-GG-H2 Comp-GG-H2-2 Syngas-cool1 Comp-syngas1 522 523 531 532 Heat exchanger Compressor Heat exchanger Compressor GASCOOL2 COMPRE_1 GASCOOL2 COMPRE_1 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 2 27 3 37 3 35 4 48 0.01 0.08 0.01 0.11 Methanol-efficiency 1: Methanol-efficiency 2: Total efficiency: 66% (with power for electrolyser) 59% (with total power) 88% Methanol 2 1.0 kg/s 535 144.0 bar Syngas-cool2 533 Heat exchanger GASCOOL2 0.40 mio. kr/MW-transferred 3 4 0.01 0.03 120 C 2 21.7 kg/s Comp-syngas2 534 Compressor COMPRE_1 4.50 mio. kr/MW 30 39 0.09 Cond-steam-1 114.3 261 C Meoh-convert 601 Meoh converter MEOH_CONVERTER ##### mio. kr/(kmol/s-syngas) 580 754 1.74 Gas composition at specific nodes (mol-%) 109.1 10.3 231.1 set-M Preheater-sy 602 Heat exchanger GASCOOL4 0.40 mio. kr/MW-transferred 8 11 0.02 793 794 3.5 bar 10.3 kg/s 601 124.5 616.7 144.0 bar Condenser-1 Syngas Condenser 640 643 Heat exchanger Heat exchanger GASCOOL4 GASCOOL4 0.40 mio. kr/MW-transferred 0.40 mio. kr/MW-transferred 3 9 5 11 0.01 0.03 Node 10 3 15 431 534 601 602 640 643 605 15 23 33 35 41 43 39 37 M-factor 1.31 4 100 C 2 124.5 kg/s Comp-recirc 605 Compressor COMPRE_1 4.50 mio. kr/MW 2 2 0.00 Species Split-meoh1 288.4 27.3 610.7 Steam 0 682 4 272 235 C Meoh-convert feed_Water Cond-steam-1 625 671 Distillation column Heat exchanger DISTILLATION_STAGE* HEATEX_1 23.52 mio. kr/(kg/s-feed) 0.40 mio. kr/MW-transferred 384 0 499 0 1.16 0.00 1 3 H2 N2 45.98 0.25 0.00 57.70 69.78 42.28 25.26 26.98 28.07 30.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 791 3.5 bar 10.2 30.6 bar Cond-steam-2 685 Heat exchanger HEATSNK0 0.40 mio. kr/MW-transferred 7 10 0.02 4 CO 42.73 0.00 22.49 0.02 1.26 1.53 1.63 1.70 1.82 792 27.3 kg/s 10.43 10.2 kg/s DH-cooler 804 Heat exchanger HEATEX_1 0.40 mio. kr/MW-transferred 9 11 0.03 6 CO2 5.24 0.00 5.09 30.18 56.10 57.00 60.87 63.33 67.68 Heatsourc-DH 4 100 C Cond-steam-1 235 C Heatsourc-DH 806 Heat exchanger HEATSRC0 0.40 mio. kr/MW-transferred 11 14 0.03 7 H2O-G 5.21 0.00 14.17 0.01 0.04 7.99 4.02 2.00 0.06 SAND 390 Cond-meoh SAND 35 Convert-cool * The distillation column is composed of 9 H2S 0.00 ##### 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.033 811 10 27.8 167.0 1.0 bar 0.033 0.70 0 806 2 DH water 167.0 1.0 bar 0 683 2 0.1 30.6 bar 0.2 0.03 0.81 0 684 4 0.1 30.6 bar Water 0 681 2 10.2 30.6 bar 18.9 Meoh-convert Methanol 1.00 SAND converter 274 311 Total several DISTILLATION_STAGE's 1636 2102 4.92 11 36 40 CH4 AR CH3OH 0.48 0.12 0.00 0.00 0.00 0.00 0.55 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.30 0.00 0.00 8.22 0.00 0.00 6.48 0.00 0.00 4.90 0.00 0.00 0.44 5.835 167.0 kg/s 90 C 1.368 167.0 kg/s 50 C 0.115 0.1 kg/s 235 C 0.025 0.1 kg/s 220 C 2.242 10.2 kg/s 220 C 602 124.5 606.5 139.0 bar 607 102.8 346.2 144.0 bar Input prices GG H2S NG_ref-cool Syngas-loop1 Syngas-meoh- Syngas-loop2 Syngas-3 Syngas-meoh Syngas-loop3 179.2 Heatsourc-DH 288.4 17.0 379.6 783 27.3 617 Heatsourc-DH 3.5 bar Cond-steam-1 Cond-steam-1 Convert-cool 2 124.5 kg/s 274 235 C 2 102.8 kg/s 158 225 C Input Electric power Price 324 kr/GJ Output cost Comparable fuel prices 781 3.5 bar 784 27.3 kg/s 10.1 10.31 Preheater-sy Mixer-syn_re Mechanical power 341 kr/GJ Output Cost flow Cost (exergy) Cost (energy) Cost (mass) Cost (volume) Fuel Price (exergy) Price (volume) 782 16.9 kg/s 4 100 C 685 30.6 bar 20.3 Preheater-sy NG 93 kr/GJ Methanol 109.1 kr/s 472 kr/GJ 532 kr/GJ 10.60 kr/kg 8.3 kr/l Methanol (commercial) 142 kr/GJ 2.5 kr/l 2 100 C Dis_stage_17 2 10.1 kg/s 158 606 2 158 0.84 SAND 29 Biomass 32 kr/GJ Oxygen 0.9 kr/s 414 kr/GJ - kr/GJ 0.05 kr/kg - kr/l Petrol 187 kr/GJ 6.6 kr/l Dis_stage_17 0 235 C Comp-recirc 158 102.8 144.0 bar 118.5 534.7 DH water 0 kr/ton Syngas 8.3 kr/s 463 kr/GJ - kr/GJ 1.53 kr/kg - kr/l Crude oil 58 kr/GJ 2.2 kr/l Cond-steam-2 0.4 MW 19 0.90 340.1 102.8 kg/s 640 139.0 bar 34 29.5 6.0 64.61 Water 32 kr/ton DH water 1.2 kr/s 70 kr/GJ 15 kr/GJ 0.00 kr/kg - kr/l Ethanol 100 kr/GJ 2.4 kr/l 0 681 4 SAND 0.369 63 C 2 118.5 kg/s 621 139.0 bar CO2 114 kr/ton Water 0 kr/s - kr/GJ - kr/GJ - kr/kg - kr/l Distillation column 293 0.64 Feed 10.1 2.217 30.6 bar 10.1 kg/s 220 C Preheater-sy 244.1 169 C Condenser-1 8.7 631 5.9 kg/s 4 169 C Preheater-sy Nomenclature: Cond-steam-2 1.33 1.00 If methanol and DH share the plant costs Condenser-1 45.7 22.79 621 631 4 (methanol and DH are the only products from the plant) - 4 705 706 13 3.5 bar 2 1.33 705 706 4 3.5 bar 6 SAND 31 114.8 482.4 643 139.0 bar 2 114.8 kg/s 4 139.0 bar 50 3.7 kg/s 147 C and the DH cost is fixed corresponding to the DH price: Output Cost flow Cost Methanol 106.9 kr/s 463 kr/Gjex Electrical power Node nr Pressure Transferred heat [MW] 14 12.8 kg/s 5 4.1 kg/s Condenser 221.3 147 C Preheater-sy DH water 12.6 kr/s 150 kr/Gjen Mass flow 137 C 137 C SAND 33 Condenser Temperature Dis_stage_1 0.03 811 8 127.0 1.0 bar Reboil-meoh2 21.3 0.03 0.74 0 805 2 DH water 127.0 1.0 bar Mechanical power 10 4.182 18.8 8.949 4.437 127.0 kg/s 1.04 127.0 kg/s 1.324 4.1 1.933 707 3.5 bar Cond-steam-2 90 C 157.4 605 2 50 C 699 3.5 bar 0.25 708 18.8 kg/s SAND 393 Condenser 102.8 139.0 bar 5.4 17.88 Condenser 700 4.1 kg/s 4 137 C 339.8 102.8 kg/s 611 139.0 bar 69.8 55.66 6.7 120.2 2 137 C Water / Methanol Methanol molar-% = 0.98 0 693 694 6 3.5 bar 3 6.0 kg/s Dis_stage_1 4 2.858 695 696 9 3.5 bar 4 8.8 kg/s 2 18.7 2.881 0.69 2.881 705 706 9 3.5 bar 10 8.8 kg/s 4 107.9 625 635 16 3.5 bar 2 Methanol molar-% = 49.7 60 C Comp-recirc Methanol/ 4 5.4 kg/s 8.283 60 C Syngas Split-syngas 621 139.0 bar 631 6.7 kg/s 4 60 C Preheater-sy Reboil-meoh2 Heat Exergy efficiency [-] 64 C set-x-2 137 C Reboil-meoh1 137 C Reboil-meoh1 234 16.3 kg/s 107 C meas_flow Methanol mass flow = 10.4 kg/s water

Page 1 and 2: Design og modellering af metanolanl

Page 3 and 4: 2 Resumé I forbindelse med DONG En

Page 5 and 6: 4 Indholdsfortegnelse 1 Abstract...

Page 7 and 8: 5 Indledning Baggrunden for dette p

Page 9 and 10: 7 Design og statisk modellering af

Page 11 and 12: Brint er specielt fordelagtig til m

Page 13 and 14: Ligning 7.1: Den specifikke varmeka

Page 15 and 16: DNA-navn: DRYER_04 Forgasser Forgas

Page 17 and 18: T Fordampning Pinch points Figur 7.

Page 19 and 20: Massestrøm af Metanol/vand-blandin

Page 21 and 22: Parameter Værdi Komponenter Evt. k

Page 23 and 24: 7.2 Anlægskonfigurationer Den opby

Page 25 and 26: 7.3 Økonomi For at kunne vurdere o

Page 27 and 28: Input-priser Kilde Elektricitet 18

Page 29 and 30: 7.4 Termoøkonomisk analyse Der er

Page 31 and 32: Komponent Produkt(er) Spild Elektro

Page 33 and 34: Tabet i fysisk exergi forekommer ho

Page 35 and 36: Anlæg 1 Total: 320 MWex (292 MW) 7

Page 37 and 38: antagelse, da naturgasnettet er try

Page 39 and 40: 246 562 112 Anlæg 1 Total: 1222 mi

Page 41 and 42: Brændsel Pris Kilde [kr/L] [kr/GJe

Page 43 and 44: Metanolomkostning [kr/GJex] 500 450

Page 45 and 46: 7.5.2 Parametervariation Nedenfor e

Page 47 and 48: Udkondenseret metanol [%] 100 95 90

Page 49 and 50: Metanolrenhed efter destillation [m

Page 51 and 52: vandkoncentrationen i syngassen fal

Page 53 and 54: Metanolexergivirkningsgrad [%] 73 7

Page 55 and 56: Metanolrenhed efter destillation [m

Page 57 and 58: Dette betyder at den metanolholdige

Page 59 and 60: Atmosfærisk forgasning (1 bar) Try

Page 61 and 62: 7.6 Diskussion I parametervariation

Page 63 and 64: 7.6.2 Alternative anlægsdesign Ned

Page 65 and 66: 8 Benyttelse af underjordiske gasla

Page 67 and 68: 8.2 Scenarier Der er undersøgt 2 s

Page 69 and 70: Ligning 8.5: Reference-el-omkostnin

Page 71 and 72: Ligning 8.13: Tidskonstant for lage

Page 73 and 74: Brintlagerbeholdning [MWh] 3000 250

Page 75 and 76: Brintlagerbeholdning [MWh] 400 350

Page 77 and 78: den time, hvor regulatorligningen b

Page 79 and 80: El-pris-funktionen [kr/MWh] 500 450

Page 81 and 82: Brintlagerbeholdning [MWh] 100 90 8

Page 83 and 84: Omkostninger [%] 100 90 80 70 60 50

Page 85 and 86: Sparede omkostninger [%] 30 25 20 1

Page 87 and 88: selvstændig investering og de omko

Page 89 and 90: Tilbagebetalingstid (beregnet ud fr

Page 91 and 92: Sparede omkostninger i nutidsværdi

Page 93 and 94: Tilbagebetalingstid [år] 15 10 5 0

Page 95 and 96: 8.4 Diskussion Resultaterne præsen

Page 97 and 98: El-pris [kr/Mwh] 400 350 300 250 20

Page 99 and 100: 9 Konklusion I den første del af r

Page 101 and 102: http://www.energyserver.net/ET1/Def

Page 103 and 104: 11 Nomenklaturliste c omkostning pe

Page 105 and 106: Design og modellering af metanolanl

Page 107 and 108: 25. Flowsheets for metanolanlæg -

Page 109 and 110: 2. Forgasserpris - Choren Choren In

Page 111 and 112: 4. El-afgifter og -tariffer GE-NET

Page 113 and 114: 6. Naturgasafgifter - DONG Energy N

Page 115 and 116: 8. Benzinforbrug til vejtransport E

Page 117 and 118: 10. Benzinafgift Benzinafgifter fra

Page 119 and 120: 12. Metanolpris Metanolpriser fra M

Page 121 and 122: Methanex Non-Discounted Reference P

Page 127 and 128: 14. Metanolproduktion, NZIC New Zea

Page 129 and 130: Maui Gas Supply Kapuni Gas Supply N

Page 131 and 132: Gas metering and letdown The proces

Page 133 and 134: Methanol Distillation Crude methano

Page 135 and 136: Product Gasoline Pipeline (250 mm N

Page 137 and 138: steam, preheat the reactants (steam

Page 139 and 140: As it is very difficult to separate

Page 141 and 142: Operational processes A schematic l

Page 143 and 144: The reaction of the synthesis gas c

Page 145 and 146: Figure 15 - Flowsheet of the MTG pr

Page 147 and 148: 15. Metanolproduktion, Nykomb Nykom

Page 149 and 150: NYKOMB SYNERGETICS 2. Methanol Plan

Page 151 and 152: NYKOMB SYNERGETICS 6. Investment Es

Page 153 and 154: NYKOMB SYNERGETICS 9. Logistics and

Page 155 and 156: 16. Metanolproduktion, Wikipedia Wi

Page 157 and 158: 18. Flowsheet for et metanolanlæg

Page 159 and 160: 20. Flowsheet for metanolanlæg - u

Page 161 and 162: 21. Flowsheet for metanolanlæg - t

Page 163 and 164: 22. Flowsheet for metanolanlæg - t


Page 167 and 168: 0 1 1 1 P 2 M type NOD* 2 1 type NO




Page 175: 0 1 1 1 P 2 M type NOD* 1 1 type NO




Page 185 and 186: 27. Flowsheet for metanolanlæg - f

Page 187 and 188: 28. Flowsheet for metanolanlæg - f

Page 189 and 190: 29. Matlab-kode til Scenarie 1

Page 191 and 192: 18-03-07 23:10 D:\DTU\Eksamensproje











Page 213 and 214: 32. DNA-kode for metanolanlæg

Page 215 and 216: metanolanlaeg.dna d:/DTU/Eksamenspr

Page 217 and 218: metanolanlaeg.dna d:/DTU/Eksamenspr

Page 219 and 220: 33. Dokumentation for tilføjede DN

Page 221 and 222: 17.121.4 Conditions ˙m1 > 0 ˙m2 <

Page 223 and 224: 9. - 10. - 11. - 12. - 13. - 14. -

Page 225 and 226: 17.123 GASIFI_3_VENZIN Gasifier wit

Page 227 and 228: 13. - 14. - 15. - 16. - 17. - 18. -

Page 229 and 230: 17.124 GASCLE_2 Syngas cleaning. Th

Page 231 and 232: 38. Compound number 39. Compound nu

Page 233 and 234: 43. - 44. - 45. - 46. - 47. - 48. -

Page 235 and 236: 17.124.5 Example struc Cleaner GASC

Page 237 and 238: 10. - 11. - 12. - 13. - 17.125.4 Co

Page 239 and 240: 7. - 8. - 9. - 10. - 11. - 12. - 13


Page 243 and 244: 11. - 12. - 13. - 14. - 15. - 16. -

Page 245 and 246: 17.128 SET_M Utility component for

Page 247 and 248: 4. - 5. - 6. - 7. - 8. - 9. - 10. -



Page 253 and 254: 17.131.2 Equations Number of equati

Page 255 and 256: 17.132 EL-MOTOR Motor with efficien

Page 257 and 258: 8. - 9. - 17.133.3 Conditions ˙m1

Page 259 and 260: 17.135 MIXER_03 Mixer for ideal gas

Page 261 and 262: 33. - 34. - 35. - 36. - 37. - 38. -

Page 263 and 264: 17.137 SET_X Utility component for


Page 267 and 268: 17.140 SET_FLOW Utillity component

Page 269 and 270: 17.142 SET_TEMP2 Utillity component

Page 271 and 272: 34. Tilføjede komponenter til DNA

Page 273 and 274: VEnzin.for c:/dna/source/ C C Param

Page 275 and 276: VEnzin.for c:/dna/source/ CA ANTED

Page 277 and 278: VEnzin.for c:/dna/source/ IF (MDOT(

Page 279 and 280: VEnzin.for c:/dna/source/ MMVAR(1)

Page 281 and 282: VEnzin.for c:/dna/source/ ENDDO DO

Page 283 and 284: VEnzin.for c:/dna/source/ $fluid O2

Page 285 and 286: VEnzin.for c:/dna/source/ C−−

Page 287 and 288: VEnzin.for c:/dna/source/ CA FKOMP

Page 289 and 290: VEnzin.for c:/dna/source/ ENDDO NIN

Page 291 and 292: VEnzin.for c:/dna/source/ C Subrout

Page 293 and 294: VEnzin.for c:/dna/source/ CALL STAT

Page 295 and 296: VEnzin.for c:/dna/source/ CA 3: Flu

Page 297 and 298: VEnzin.for c:/dna/source/ C C C M_B

Page 299 and 300: VEnzin.for c:/dna/source/ C C SETFL

Page 301 and 302: VEnzin.for c:/dna/source/ C C GASCO

Page 303 and 304: VEnzin.for c:/dna/source/ RES(5) =

Page 305 and 306: VEnzin.for c:/dna/source/ c c c E2=

Page 307 and 308: VEnzin.for c:/dna/source/ C C HEATE

Page 309 and 310: VEnzin.for c:/dna/source/ $ ’$\\d

Page 311 and 312: VEnzin.for c:/dna/source/ c 1 = Wat

Page 313 and 314: VEnzin.for c:/dna/source/ CA 4: Fin

Page 315 and 316: VEnzin.for c:/dna/source/ CL K_MED

Page 317 and 318: VEnzin.for c:/dna/source/ CA MEDIE

Page 319 and 320: VEnzin.for c:/dna/source/ CA −4 :

Page 321 and 322: VEnzin.for c:/dna/source/ C ENDDO E

Page 323 and 324: VEnzin.for c:/dna/source/ MEDIE(2)

Page 325 and 326: VEnzin.for c:/dna/source/ C C 400 C

Page 327 and 328: VEnzin.for c:/dna/source/ GOTO 9999

Page 329 and 330: VEnzin.for c:/dna/source/ MEDIE(1)


Page 333 and 334: VEnzin.for c:/dna/source/ RES(1) =



Page 339 and 340: 35. Metanol (fluid) til DNA - Fortr

Page 341 and 342: methanol.for d:/DTU/Eksamensprojekt









methanol

exchanger

output

goto

component

electrolyser

compressor

input

gasifier

syngas

modellering

bilag

etd.dtu.dk

Design og modellering af metanolanlæg til VEnzin-visionen Bilag

Design og modellering af metanolanlæg til VEnzin-visionen Bilag ... View more Design og modellering af metanolanlæg til VEnzin-visionen Bilag

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Design og modellering af metanolanlæg til VEnzin-visionen Bilag Design og modellering af metanolanlæg til VEnzin-visionen Bilag